Process for reforming hydrocarbons

ABSTRACT

A process for the production of synthesis gas by the use of autothermal reforming in which tail gas from downstream Fischer-Tropsh synthesis is hydrogenated and then added to the autothermal reforming stage.

This is a continuation of U.S. application Ser. No. 14/129,244, filed onJan. 31, 2014, which is a 371 of International Application No.PCT/EP2012/061809, filed on Jun. 20, 2012, which claims priority toDenmark Application No. PA 2011 00485, filed on Jun. 29, 2011, EuropeanApplication No. 11009101.4, filed on Nov. 26, 2011, and DenmarkApplication No. PA 2011 00947, filed on Dec. 6, 2011.

FIELD OF THE INVENTION

The present invention relates to a process for the production ofsynthesis gas used for the production of hydrocarbons by Fischer-Tropschsynthesis. The invention relates in particular to a process for theproduction of synthesis gas by the use of autothermal reforming in whichtail gas from a downstream process, in particular Fischer-Tropshsynthesis, is hydrogenated and then added to the autothermal reforming.In a more general aspect the invention encompasses the removal ofolefins in a gas to reduce metal dusting of metal parts in contact withthe gas, particularly for the reduction of metal dusting in ATR, CPO orPOx and other downstream equipment through which the gas is passed.

BACKGROUND OF THE INVENTION

The production of synthesis gas for Fischer-Tropsch synthesis istypically obtained by passing a hydrocarbon feed through primary andsecondary reforming stages. The primary reforming is often conducted intubular steam reformers or heat exchange reformers, while the secondaryreforming is typically conducted in autothermal reformers. Whencombining a heat exchange reformer with a subsequent autothermalreformer, the hot effluent gas from the autothermal reformed is usuallyused as heating medium in the heat exchange reformer. It is known torecycle tail gas from Fischer-Tropsch synthesis as part of thehydrocarbon feed used to produce the synthesis gas in the primary andsecondary reforming stages. Tail gas can be added prior to the primaryreforming or to the primary reformed gas before entering the secondaryreforming (typically autothermal reforming).

Tail gas from Fischer-Tropsch synthesis contains hydrogen, carbonmonoxide, carbon dioxide as well as light hydrocarbons in the form ofparaffins such as methane, ethane, propane and not least olefins such aspropylene. The tail gas may also include alcohols and other higherhydrocarbons of both paraffinic and olefinic nature. It is known thatthe addition of such tail gas to the synthesis gas production sectionenables that there is sufficient carbon dioxide during the reforming toachieve the desired H₂/CO molar ratio, typically about 2.0.

As used herein “tail gas” means off-gas from the Fischer-Tropschsynthesis stage which is not re-used in said stage.

Hydrogenation of tail gas is known in the art. For instance, in GB632386 tail gas from Fischer-Tropsch synthesis is hydrogenated in orderto increase the otherwise low heating value of this gas caused by thepresence of i.a. carbon dioxide, carbon monoxide and hydrogen.

WO-A-0142175 discloses a process in which tail gas is hydrogenated inorder to saturate any unsaturated hydrocarbons and is then reformed in aseparate steam reformer. The hydrogenation serves to decrease thetendency towards coking in the subsequent high temperature treatment ofthe steam reformer, since the tendency to coking in said reformer isgreater when unsaturated hydrocarbons are present in the tail gas. Theresulting reformed tail gas may subsequently also be passed to anautothermal reformer. Accordingly, a steam reformer is used between thehydrogenation stage and the autothermal reformer.

EP-A-1860063 discloses a process in which off-gas from Fischer-Tropschsynthesis where olefins present in the off-gas are first hydrogenatedand then converted to hydrogen by a reforming process. Olefins arehydrogenated because of carbon deposition or coking of catalysts used inthe hydrogen manufacturing unit and which form hot spots on the catalystand the reformer reactor tubes. Thus, olefins are removed to avoidcoking in a steam reformer having reformer tubes such as a firedreformer.

SUMMARY OF THE INVENTION

We have now found out that the addition of tail gas to the autothermalreformer (ATR), or catalytic partial oxidation reactor (CPO), ornon-catalytic partial oxidation reactor (POx), which is desirable inorder to adjust the H₂/CO ratio in the synthesis gas, has the severedrawback of promoting metal dusting corrosion, particularly in theburner parts of the ATR or CPO, yet by hydrogenation of the tail gasprior to its direct addition to the ATR such metal dusting issignificantly reduced. It has come as a surprise to the applicant thatthe removal of particularly olefins in the tail gas via hydrogenationconveys the critical advantage of significantly reducing theaggressiveness of the tail gas and hence reducing or eliminating metaldusting in the ATR, or CPO or POx. At the same time the benefits ofusing tail gas to adjust the H₂/CO ratio are maintained.

The reduction or elimination of metal dusting in an apparatus, e.g. ATR,CPO or POx, according to the simple, economical and elegant solutionprovided by the present invention translates directly into the reductionor elimination of costly down-time periods in the plant and reducesthereby maintenance costs. Metal dusting has otherwise been mitigatedthrough the use of resistant alloy compositions or metallic coatingsthat form protective surfaces under metal dusting conditions, and/or byoperating the reformer at less metal dusting aggressive conditions butwhich on the other hand impair the process. Yet even the use ofexpensive and otherwise effective alloys against metal dusting such asInconel 690 cannot withstand metal dusting attack when exposed to tailgas from Fischer-Tropsch synthesis.

Metal dusting is a type of metallic corrosion that may be encounteredwhen gases containing carbon monoxide come into contact with metalsabove ca. 400° C., particularly in the range 400-800° C. Metal dustingconveys the disintegration of metals to dust and is describedextensively in the literature.

Metal dusting is a highly complex corrosion process which is notcompletely understood. However, it is often represented by the followingreaction:

CO+H₂→C+H₂O  (1)

The formed carbon results in corrosion of the construction materialpossibly by a mechanism including carbide formation and/or dissolutionof the carbon in the metal material.

Carbon formation via the exothermic reactions 2CO→C+CO₂ (Boudouardreaction) and CO+H₂→C+H₂O (CO-reduction) is a precursor for metaldusting (MD) corrosion. The exothermic reactions are favoured at lowtemperatures. However, the reaction rates are higher at highertemperatures. As a result, the MD potential for a given gas will behighest in a medium temperature range, typically in the range of about400-800° C.

It has to be appreciated, however, that metal dusting and coking are twodifferent phenomena. While metal dusting refers to catastrophiccorrosion of metal parts, coking is associated with the catalyst. Cokingrefers more specifically to carbon formation negatively affecting thecatalyst of a steam reformer such as a tubular reformer due to formationof carbonaceous elements that deposit and dissociate on the nickelsurface or support material of the steam reforming catalyst (typically anickel-based catalyst). This may convey also the development of hotspots in the tubes containing the catalyst. Accordingly, for the skilledperson metal dusting and coking are two different phenomena: while ithas been known for long that the presence of olefins causes cokedeposition in catalyst beds, no one has ever seen nor expected thatolefins are also responsible for causing such a different phenomenon asmetal dusting.

Accordingly, in a first aspect of the invention we provide a process forthe production of synthesis gas from a hydrocarbon feedstock withreduced metal dusting potential in at least the burner parts of anautothermal reformer (ATR), catalytic partial oxidation reactor (CPO),or partial oxidation reactor (POx) comprising: passing said hydrocarbonfeedstock through an ATR, CPO or POx, and withdrawing a stream of hoteffluent synthesis gas from the ATR, CPO or POx, passing tail gas from aFischer-Tropsch synthesis stage through a hydrogenation stage to producea hydrogenated tail gas and adding the hydrogenated tail gas directly tosaid ATR, CPO or POx.

The hydrogenation of the tail gas results in a gas that protects theATR, CPO or POx from metal dusting, particularly for ATR and CPO theburner metal parts located at the inlet of the reactor and thus upstreamthe catalyst bed, as it unexpectedly turns out that the absence ofolefins makes a gas less aggressive with respect to metal dustingcorrosion.

Hence, there is provided in an elegant and simple manner a solution tothe long-standing problem of metal dusting of metal parts in the ATR,CPO or POx, particularly burner parts of the ATR, which were encounteredwhen incorporating tail gas from Fischer-Tropsch synthesis into theprocess.

As used herein the term “reduced metal dusting potential in at least theburner parts of an autothermal reformer (ATR), catalytic partialoxidation reactor (CPO), or partial oxidation reactor (POx)” means thatthe metal dusting potential is reduced in any metal part within thereactor being in contact with the process gas fed to the it (ATR, CPO,POx) including burner metal parts, particularly for ATR or POx. It wouldbe understood by the skilled person that ATR and POx imply the use of aburner at the top of the reactor. ATR and CPO use a catalyst bed belowthe combustion zone. CPO means a catalytic reactor or catalytic gasifierwhich does not always require the use of a burner, but a mixer instead.Further, in a POx (gasifier) there is no use of catalyst. The term ATRincludes secondary reformers.

Since the tail gas contains carbon monoxide, carbon dioxide, hydrogen,various hydrocarbons including olefins and a range of other componentsas described above, the gas is converted by reducing the olefinconcentration by hydrogenation according to the following reactionC₃H₆+H₂

C₃H₈. The reaction is given for propylene hydrogenation buthydrogenation of other olefins takes place according to a similarreaction.

Catalysts suitable for selectively hydrogenating the olefins tosaturated hydrocarbons are preferably based on copper, for instance aCu/ZnO catalyst, or a combination of copper and a noble metal, forinstance platinum or palladium. A copper based catalyst, such as Cu/ZnOcatalyst, is particularly active in the selective hydrogenation ofolefins to paraffins with reduced formation or without the formation ofmethanol or higher alcohols having two or more carbon atoms in theirstructure.

In connection with the above and below embodiments, the hydrogenation ispreferably conducted in a cooled reactor, particularly at a temperaturein the range 100-150° C. or higher, for instance 185° C. This enableshigh conversion of olefins such as C₃H₆ and C₄H₈ while at the same timeavoiding significant formation of methanol or higher alcohols and otherby-products. Alternatively, the hydrogenation is conducted in anadiabatic reactor in which the inlet temperature is preferably in therange 70-120° C., more preferably 80-100° C., and the outlet temperatureis 120-210° C., preferably 140-190° C., more preferably 150-185° C.

The pressure in the hydrogenation step is in the range 20-70 bar,preferably 20-50 bar, more preferably 20-40 bar.

In one embodiment of the invention said hydrocarbon feedstock is a gasthat has passed through at least one adiabatic pre-reforming stage.

Adiabatic pre-reforming is preferably conducted in a fixed bed reactorcontaining a reforming catalyst, thereby converting all higherhydrocarbons into a mixture of carbon oxides, hydrogen and methane. Thisendothermic process is accompanied by the equilibration of exothermicmethanation and shift reactions. Removal of higher hydrocarbons allows ahigher preheat temperature to the subsequent steam reforming.

In another embodiment of the invention said hydrocarbon feedstock is agas that has passed through at least one steam reforming stage. Thesteam reforming stage may for instance be tubular reforming (steammethane reforming, SMR) or heat exchange reforming (convectivereforming).

In yet another embodiment, the invention encompasses also a processwherein said hydrocarbon feedstock is a gas mixture resulting fromdividing a raw hydrocarbon feed gas into two streams, passing the firststream through at least one steam reforming stage to form a primaryreformed gas, using the second stream as a by-pass stream to said steamreforming stage, and subsequently combining said primary reformed gaswith the by-pass stream to form said hydrocarbon feedstock.

According to this embodiment, steam reforming is arranged in series withthe ATR, CPO or POx.

In a separate embodiment, an arrangement where steam reforming isarranged in parallel with the ATR, CPO or POx, is also provided. Hence,the process comprises dividing a raw hydrocarbon feed gas into twostreams, by which one of the streams formed becomes said hydrocarbonfeedstock, and passing the other stream through at least one steamreforming stage to form a reformed gas.

In another embodiment in combination with anyone of the above or belowembodiments, there is provided a process wherein the steam reformingstage is heat exchange reforming, and where at least a portion of thehot effluent synthesis gas from the ATR, or CPO, or POx stage is used asheating medium in said heat exchange reforming.

Hence, one preferred embodiment is a process in which a heat exchangereformer is arranged upstream and in series with an ATR or CPO,preferably an ATR. The raw hydrocarbon feed, for example desulphurisednatural gas, is mixed with steam and the resultant mixture is directedto the catalyst side of the heat exchange reformer. In the heat exchangereformer, the gas is then steam reformed according to the reactions:CH₄+H₂O⇄CO+3H₂ and CO+H₂O⇄CO₂+H₂. The gas leaving the heat exchangereformer is close to chemical equilibrium for the reactions above.Typically, the exit temperature is 600-850° C. or preferably 675-775° C.The primary reformed gas leaving the heat exchange reformer is passed tothe ATR or CPO. In the reactor (ATR or CPO) also oxygen and in somecases a small amount of steam is added. Synthesis gas is formed by acombination of steam reforming and partial oxidation in the reactor. Thegas leaving the reactor is free of oxygen and generally the abovereactions are close to chemical equilibrium. The temperature of this hoteffluent gas from e.g. an autothermal reformer is between 950 and 1100°C., typically between 1000 and 1075° C.

This hot effluent gas leaving the reactor comprises carbon monoxide,hydrogen, carbon dioxide, steam, residual methane, and various othercomponents including nitrogen and argon. This synthesis gas is passed tothe non-catalytic side of the heat exchange reformer, where it is cooledby supplying heat to the catalytic side of the heat exchange reformer byindirect heat exchange. The exit temperature from this side of the heatexchange reformer would typically be in the range from 500-800° C.

It also follows that in another preferred embodiment a heat exchangereformer is arranged in parallel with an ATR, CPO or POx, preferably anATR, and hot effluent synthesis gas from the ATR, CPO or POx is used toprovide heat for the endothermic reforming reactions in the heatexchange reformer.

In the parallel arrangement said hot effluent synthesis gas is combinedwith said reformed gas before, during or after said hot effluentsynthesis gas has delivered heat to the heat exchange reforming.Preferably, said hot effluent synthesis gas is combined with saidreformed gas before it has delivered heat to the heat exchangereforming.

In yet another embodiment in combination with one of the above or belowembodiments, the process comprises also adding a stream comprising steamto said hot effluent synthesis gas, said reformed gas, or the combinedstream of hot effluent synthesis gas and reformed gas.

Hence, regardless of whether the heat exchange reformer is arranged inseries or in parallel with the ATR, CPO or POx, steam is introduced tothe gas from the ATR, CPO or POx delivering heat to the heat exchangereformer. This enables reduction of metal dusting in the metal parts,particularly the shell side, of the heat exchange reformer, particularlywhere the heat exchange reformer is in series arrangement with the ATR,CPO or POx. This stream comprising steam contains preferably more than90 vol % of steam (H₂O in the vapour phase), more preferably more than95%, and most preferably more than 99%. Preferably, the temperature ofthe hot effluent synthesis gas is 950 to 1050° C., more preferably 1025°C., while the steam added is preferably at 271° C. at 55 barg, thusresulting in a temperature of the mixed stream, i.e. hot effluentsynthesis gas combined with stream comprising steam, of 900 to 990° C.

In a further embodiment in combination with anyone of the above or belowembodiments, the at least one adiabatic pre-reforming stage is conductedprior to dividing said raw hydrocarbon feed. Hence, prior to dividingthe raw hydrocarbon feed gas in separate streams in the series orparallel arrangements, adiabatic pre-reforming of the raw hydrocarbonfeed (typically comprising methane and higher hydrocarbons) isconducted.

In an another embodiment in combination with anyone of the above orbelow embodiments, the process comprises also mixing the hydrogenatedtail gas with the hydrocarbon feedstock prior to conducting reforming inthe ATR, CPO or POx; or alternatively, adding the hydrogenated tail gasto the ATR, CPO or POx as a separate stream.

In connection with the operation of the series arrangement as describedabove, there is also provided a process comprising mixing thehydrogenated tail gas with said by-pass stream prior to conductingreforming in the ATR, CPO or POx; or alternatively, mixing thehydrogenated tail gas with said primary reformed gas.

In yet a further embodiment in combination with anyone of the aboveembodiments, the process further comprises of converting the synthesisgas into liquid hydrocarbons, particularly diesel via Fischer-Tropschsynthesis.

In a second aspect the invention encompasses the use of hydrogenatedtail gas from a Fischer-Tropsch synthesis stage as means for reductionof metal dusting in an autothermal reformer (ATR), catalytic partialoxidation reactor (CPO), or partial oxidation reactor (POx).

Hence, according to this aspect the invention encompasses the use of aknown substance (hydrogenated tail gas) to obtain the surprisingtechnical effect of reduced metal dusting in an ATR, CPO or POx.Alternative expensive methods such as the provision of resistant alloycompositions or metallic coatings that form protective surfaces undermetal dusting conditions are thus avoided.

Tail gas from Fischer-Tropsch synthesis is hydrogenated, therebyconverting olefins (alkenes) into alkanes, and thus unexpectedly resultsin reduction of metal dusting in at least the burner parts of thereactor compared to a situation where the tail gas is added directly,without being hydrogenated. Since the use of tail gas is desirable inorder to adjust the H₂/CO ratio in the synthesis gas, this is nowpossible without risking expensive downtime periods and maintenancecosts in the ATR, CPO or POx due to metal dusting issues.

The hydrogenated tail gas contains preferably less than 1 mol % olefins,more preferably less than 1 mol %, most preferably below 0.5 mol %, suchas less than 0.2 mole %, or less than 0.1 mole %.

The hydrogenated tail gas is added directly to the ATR, CPO or POx, asillustrated in the enclosed Figures. The term “directly” means withoutany intermediate processes which change the chemical composition of thehydrogenated tail gas, e.g. without a steam reformer between saidhydrogenation stage and said ATR, CPO or POx.

In a broader aspect the invention encompasses also a method for reducingmetal dusting in an apparatus, said apparatus containing an off-gas,said method comprising the removal of olefins from said off-gas. Inparticular, olefins are removed by hydrogenation thereof. The method isparticularly useful for the reduction of metal dusting in ATR, CPO orPOx and other downstream equipment through which off-gas is passed. Theinvention encompasses a method for the reduction of metal dusting in anATR, CPO or POx and further downstream equipment by removing the contentof olefins in an off-gas to be passed through the ATR, CPO or POx.

Preferably, said step of removing the content of olefins is ahydrogenation stage.

As used herein the term “further downstream equipment” means waste heatboiler and/or steam superheater located downstream the ATR, CPO or POxand which are used for cooling the synthesis gas under the production ofsteam.

As used herein the term “removing the content of olefins” means reducingthe content of olefins in the gas to less than 0.2 mole %, preferablyless than 0.1 mole %.

As used herein the term “off-gas” means any gas containing hydrocarbonsand olefins, which has to be reformed in the ATR, CPO or POx to form asynthesis gas comprising hydrogen and carbon monoxide. The off-gas ispreferably tail gas from Fischer-Tropsch synthesis or tail gas fromdownstream process for production of gasoline, such as a process inwhich gasoline is produced from oxygenates comprising methanol anddimethyl ether, for instance via the so-called TIGAS process asdisclosed in U.S. Pat. No. 4,520,216 and U.S. Pat. No. 4,481,305.

The invention encompasses also the use of a gas free of olefins as meansfor the reduction of metal dusting of the metal parts of apparatus indirect contact with the gas. Preferably the apparatus in direct contactwith the gas is an ATR, CPO or POx. Preferably, the gas is an off-gas;i.e. the waste gas from an industrial process such as gasoline synthesisas defined above.

As used herein and in accordance above the term “gas free of olefins” agas with less than 0.2 mole %, preferably less than 0.1 mole % olefins.

As used herein the term “in direct contact with the gas” means that thegas free of olefins is added directly to the equipment or to a separatehydrocarbon feedstock without first being passed through an intermediatestage of reforming, such as steam reforming.

BRIEF DESCRIPTION OF THE DRAWINGS

The invention is further illustrated by reference to the accompanyingfigures.

FIG. 1 shows a schematic view of the invention when using a stand-aloneautothermal reformer yet including a pre-reformer.

FIG. 2 shows heat exchange reforming and autothermal reforming in serieswith hydrogenated tail gas addition to the primary reformed gas.

FIG. 3 shows a process with by-pass of the primary reforming stage, withaddition of hydrogenated tail gas to the by-pass stream, or to thecombined stream of primary reformed gas and by-pass stream.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

The accompanying FIG. 1 shows a general schematic view of an embodimentfor the production of synthesis gas for Fischer-Tropsch synthesis usinga stand-alone autothermal reformer. Clean (free of sulphur and otherpoisons to reforming catalysts) hydrocarbon feed gas 100 such as naturalgas or other hydrocarbon containing gas source is mixed with processsteam 110, optionally partly via saturator/humidifier. The mixture ispreheated and pre-reformed adiabatically in pre-reformer 300 in order toconvert any higher hydrocarbons into H₂, CO, CO₂ and CH₄. This resultinghydrocarbon feedstock mixture 120 is fed to the autothermal reformer 400together with oxygen 130, protection steam 140 and hydrogenated tail gas150. From the autothermal reformer 400 at hot effluent of synthesis gas160 is withdrawn and further processed to form the synthesis gas feed tothe downstream Fischer-Tropsch section 500. Liquid hydrocarbons 170 areproduced and tail gas recycle stream 180 is passed through hydrogenatingstage 600 prior to entering the autothermal reformer 400. Notably,hydrogenated tail gas is added directly from the hydrogenator to theautothermal reformer 400.

In FIG. 2, a mixture of the raw hydrocarbon feed gas and steam 10 ispassed to heat-exchange reformer 25 where it is catalytically steamreformed and thereafter leaves the heat-exchange reformer as stream 30.The primary reformed gas stream 30 is mixed with hydrogenated tail gas65 from Fischer-Tropsch section 150 forming the ATR feed stream 70. Themixed stream 70 is fed to an autothermal reformer 75 with oxidant 80 andprotection steam (not shown) also being supplied. The primary reformedgas is partially combusted and brought towards equilibrium overreforming catalyst in the autothermal reformer 75. The hot effluentsynthesis gas 110 from the autothermal reformer is passed through theheat exchange reformer 25. The synthesis gas is cooled by heat exchangewith the gas undergoing reforming over the catalyst in the heat-exchangereformer 25. The thus cooled synthesis gas leaves the heat exchangereformer as stream 120 and is further processed to form the synthesisgas feed to the Fischer-Tropsch section 150 downstream. Liquidhydrocarbon products 140 are withdrawn together with a tail gas recyclestream 60. The tail gas recycle stream 60 passes through hydrogenator160 to form hydrogenated tail gas stream 65 before being combined withprimary reformed gas 30. Notably, hydrogenated tail gas is addeddirectly from the hydrogenator to the autothermal reformer 400.

In FIG. 3, a mixture of raw hydrocarbon feed gas (10) is divided intotwo streams 20 and 40. The first stream 20 is fed to the heat-exchangereformer 25 where it is catalytically steam reformed and thereafterleaves the heat-exchange reformer as primary reformed gas 30. The secondstream 40 is preheated in a heat exchanger 45 and bypasses the heatexchange reformer. The primary reformed gas 30 is mixed with thepreheated second stream 50. Hydrogenated tail gas 65 is added to thismixed stream or to the preheated second stream 50 thus forming the ATRfeed stream 70. The ATR feed stream is fed to the autothermal reformer75 to which oxidant 80 and protection steam (not shown) are alsosupplied. The ATR feed stream is partially combusted and brought towardsequilibrium over reforming catalyst in the autothermal reformer 75. Thehot effluent synthesis gas 110 is passed through the heat exchangereformer 25. The mixture stream is cooled by heat exchange with the gasundergoing reforming over the catalyst in the heat-exchange reformer 25.The thus cooled synthesis gas leaves the heat exchange reformer asstream 120 and is further processed to form the synthesis gas feed tothe Fischer-Tropsch section 150 downstream. Liquid hydrocarbon products140 are withdrawn together with a tail gas recycle stream 60. The tailgas recycle stream 60 passes through hydrogenator 160 to formhydrogenated tail gas stream 65 which is then combined with primaryreformed gas 30 or by-pass stream 50. Alternatively, the hydrogenatedtail gas 65 may also be added to the primary reformed stream 30.Notably, hydrogenated tail gas is added directly from the hydrogenatorto the autothermal reformer 400.

EXAMPLE

Two tests were made in the same experimental setup: An 800 mm longsample of Inconel 690 was placed in a reactor. The reactor was placed inan oven with three heating zones. The temperature of the Inconel 690sample varied with the position in the oven. The sample temperatureswere 200 to 640° C. The sample was exposed to a continuous flow of gaswith the composition given in Table 1 as Test 1. The flow rate was 100Nl/h. The pressure was 29 barg. The conditions were kept for 626 hours.The sample was examined after the test using stereo microscope andscanning electron microscope. The sample was attacked by metal dustingcorrosion.

The second test was made analogous to the first test, with theexceptions that the gas composition used was as given in Table 1 as Test2 and the conditions were kept for 672 hours. Examination of the sampleafter the test showed that the sample was not attacked by metal dustingcorrosion.

TABLE 1 Gas compositions (mole %) Component Test 1 Test 2 Hydrogen 12.112.1 Water 22.6 22.6 Carbon 6.9 6.9 monoxide Carbon 7.8 7.8 dioxideEthylene 0.14 0 Ethane 0 0.14 Methane 49.8 49.8 Propane 0.45 0.451-Butene 0.21 0 Butane 0 0.21

The two gas compositions in the two tests are identical with theexception that the gas in test 1 contains the olefins (alkenes), whereasthe gas in test 2 contains the corresponding alkanes. Metal dustingattack occurs in Test 1 but not in Test 2, which is of longer duration.

The presence of alkenes makes a gas more aggressive with respect tometal dusting corrosion. Thus, the use of a hydrogenated tail gasconveys the reduction or elimination of metal dusting compared to asituation where tail gas is used without being hydrogenated.

What is claimed is:
 1. A process for the production of synthesis gasfrom a hydrocarbon feedstock with reduced metal dusting in at least theburner parts of an autothermal reformer (ATR), catalytic partialoxidation reactor (CPO), or partial oxidation reactor (POx), the processcomprising the steps of: passing said hydrocarbon feedstock through anATR, CPO or POx, and withdrawing a stream of hot effluent synthesis gasfrom the ATR, CPO or POx; passing tail gas from a Fischer-Tropschsynthesis stage through a hydrogenation stage to produce a hydrogenatedtail gas; and adding the hydrogenated tail gas directly to said ATR, CPOor POx.
 2. The process according to claim 1, wherein said hydrocarbonfeedstock is a gas that has passed through at least one adiabaticpre-reforming stage.
 3. The process according to claim 1, wherein saidhydrocarbon feedstock is a gas that has passed through at least onesteam reforming stage.
 4. The process according to claim 1, wherein saidhydrocarbon feedstock is a gas mixture resulting from dividing a rawhydrocarbon feed gas into two streams, passing the first stream throughat least one steam reforming stage to form a primary reformed gas, usingthe second stream as a by-pass stream to said steam reforming stage, andsubsequently combining said primary reformed gas with the by-pass streamto form said hydrocarbon feedstock.
 5. The process according to claim 1,comprising dividing a raw hydrocarbon feed gas into two streams, bywhich one of the streams becomes said hydrocarbon feedstock, and passingthe other stream through at least one steam reforming stage to form areformed gas.
 6. The process according to claim 3, wherein the steamreforming stage is heat exchange reforming, and where at least a portionof the hot effluent synthesis gas from the ATR, CPO, or POx is used asheating medium in said heat exchange reforming.
 7. The process accordingto claim 6, wherein said hot effluent synthesis gas is combined withsaid reformed gas before, during or after said hot effluent synthesisgas has delivered heat to the heat exchange reforming.
 8. The processaccording to claim 7, comprising adding a stream comprising steam tosaid hot effluent synthesis gas, to said reformed gas, or to thecombined stream of hot effluent synthesis gas and reformed gas.
 9. Theprocess according to claim 4, wherein at least one adiabaticpre-reforming stage is conducted prior to dividing said raw hydrocarbonfeed.
 10. The process according to claim 1, comprising mixing thehydrogenated tail gas with the hydrocarbon feedstock prior to conductingreforming in the ATR, CPO or POx.
 11. The process according to claim 1,comprising adding the hydrogenated tail gas to the ATR, CPO or POx as aseparate stream.
 12. The process according to claim 4, comprising mixingthe hydrogenated tail gas with said by-pass stream prior to conductingreforming in the ATR, CPO or POx.
 13. The process according to claim 4,comprising mixing the hydrogenated tail gas with said primary reformedgas.
 14. The process according to claim 1, further comprising convertingthe synthesis gas into liquid hydrocarbons via Fischer-Tropschsynthesis.